CN103492581A - Method for producing directly transesterified oil or fat - Google Patents
Method for producing directly transesterified oil or fat Download PDFInfo
- Publication number
- CN103492581A CN103492581A CN201280019208.7A CN201280019208A CN103492581A CN 103492581 A CN103492581 A CN 103492581A CN 201280019208 A CN201280019208 A CN 201280019208A CN 103492581 A CN103492581 A CN 103492581A
- Authority
- CN
- China
- Prior art keywords
- grease
- enzyme catalyst
- reaction
- crystal
- enzyme
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/64—Fats; Fatty oils; Ester-type waxes; Higher fatty acids, i.e. having at least seven carbon atoms in an unbroken chain bound to a carboxyl group; Oxidised oils or fats
- C12P7/6436—Fatty acid esters
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Zoology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Wood Science & Technology (AREA)
- Biotechnology (AREA)
- Microbiology (AREA)
- General Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
- Biochemistry (AREA)
- Bioinformatics & Cheminformatics (AREA)
- General Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- Genetics & Genomics (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Fats And Perfumes (AREA)
Abstract
The present invention relates to a method for producing a directly transesterified oil or fat with high efficiency by performing a direct transesterification reaction of a raw oil or fat while dispersing an enzyme catalyst in the raw oil or fat to produce the directly transesterified oil or fat and then separating the directly transesterified oil or fat from the enzyme. Specifically, provided is a process for producing a directly transesterified oil or fat, which is characterized in that, in a direct transesterification reaction using an enzyme catalyst, the enzyme catalyst exists in a flowable state in a raw oil or fat in the reaction system and the enzyme catalyst is sedimented in the reacted oil or fat utilizing the difference in specific gravity between crystals produced by the reaction and the enzyme catalyst without melting the crystals to thereby separate the crystals from the enzyme catalyst.
Description
Technical field
The present invention relates to a kind of manufacture method of using the grease of direct transesterification reaction.
Background technology
Direct transesterification reaction is to carry out the reaction of transesterification reaction when the high-melting-point compositions such as trisaturated glyceride in making grease are separated out as crystal, by increasing trisaturated glyceride (SSS) and the triunsaturated glyceride (UUU) in grease, can produce the grease with distinctive composition.
The method of described direct transesterification reaction mainly contains two kinds.First method is as shown in record in non-patent literature 1, it is the method for the tower that uses immobilization that the enzyme catalyst with transesterification reaction function arranged and the generation of carrying out crystal and the tank that separates, second method, as shown in record in patent documentation 1, is the method that makes catalyzer disperse and be reacted when producing crystal in grease.
As the use of described first method the method for tower and tank be to make as the aqueous grease of raw material through by the catalyzer immobilization being possessed to the tower of transesterification reaction function, make produced high-melting-point composition at the tank intercrystalline, make the remaining aqueous grease as the low melting point composition again through tower, by repeatedly carrying out this kind of operation, can carry out continuously direct transesterification reaction.But, the inventor etc. confirm, consequently, utilize the method to be difficult to the crystal (SSS) produced in tank is fully separated with aqueous grease, in addition, can make to contain the aqueous grease fusing of the crystal that can't separate, in the situation that through tower, directly the problem that direct transesterification reaction can not be carried out, according to circumstances appearred in the reaction efficiency variation of transesterification reaction.
On the other hand, in the following method as described second method,, catalyzer is dispersed in the aqueous grease of raw material, carry out direct transesterification reaction when producing crystal, owing to catalyzer being scattered in crystal and aqueous grease, therefore do not need crystal is separated with aqueous grease, can effectively carry out direct transesterification reaction.
In described direct transesterification reaction, operable catalyzer is divided into two kinds of the chemical catalysts such as sodium methylate and enzyme catalysts haply.Described chemical catalyst is low and active high due to cost, therefore extensively utilized, if yet directly in transesterification reaction, using chemical catalyst, can produce dialkyl ketone etc. and be considered to unwell material, therefore in the situation that the grease of gained will be had to problem (patent documentation 2) especially for edible.On the other hand, if directly in transesterification reaction, using enzyme catalyst, can not produce the materials such as dialkyl ketone such while using chemical catalyst, so the utilization of enzyme catalyst is extensive.
For example, if put down in writing in patent documentation 1, enzyme catalyst is scattered in the aqueous grease of raw material, carry out direct transesterification reaction when producing crystal, react grease and will become and mix the state that the crystal produced in direct transesterification reaction, aqueous grease and enzyme catalyst are arranged.Then, after described reaction finishes, if want to isolate enzyme catalyst from the admixture of crystal, aqueous grease and enzyme catalyst, because crystal is solid, therefore be difficult to only enzyme catalyst be separated.Put down in writing in described patent documentation 1 to utilize and removed by filter enzyme, therefore the inventor waits and attempts practically, consequently, to filter as the crystal of solid and enzyme catalyst utilization that fully to be separated in be in fact impossible, the quantitative change of the direct transesterification reaction grease that is substantially devoid of enzyme catalyst of gained obtains quite few.
In addition, if in order to separate enzyme catalyst by crystal melting, can carry out random transesterification reaction, therefore can't be by crystal melting.
In addition, even enzyme catalyst is leached together with crystal, in order to separate enzyme catalyst from crystal, also only have crystal melting, also can estimate in this situation, when the fusing of crystal, crystal can carry out the transesterify outside original idea because of enzyme catalyst.
Like this, carry out the method for direct transesterification reaction in enzyme catalyst is scattered in to grease and when producing crystal in, following very large problem has appearred,, be difficult in the generation that realizes crystal, effectively separate enzyme catalyst from the crystal of gained.
The prior art document
Patent documentation
Patent documentation 1: Japanese kokai publication sho 60-078586 communique
Patent documentation 2: No. 2009/012982nd, International Publication
Non-patent literature
Non-patent literature 1:Enzyme and Microbial Technology27(2000) 302-311 page
Summary of the invention
The problem that invention will solve
The object of the invention is to, a kind of method is provided, in the situation that in enzyme catalyst being scattered in to the grease of raw material and carry out direct transesterification reaction, the direct transesterify grease generated can be separated with enzyme, effectively obtain described direct transesterify grease.
The means of dealing with problems
The inventor etc. conduct in-depth research in order to address the above problem repeatedly, consequently, by be conceived to exist the fact of difference in specific gravity between the crystal of enzyme catalyst and the solid fat that directly produces in transesterification reaction, utilize the sedimentation in the reaction grease of this proportion official post enzyme catalyst, and first successfully by enzyme catalyst and crystal separation.
The present invention is based on opinion as above and completes.
; the present invention relates to a kind of manufacture method of direct transesterify grease; it is characterized in that; in the direct transesterification reaction of using enzyme catalyst; in the raw oil material of enzyme catalyst in reaction system existing by mobile state; do not melt the crystal generated by described reaction, utilize proportion official post enzyme catalyst sedimentation in reacting grease of crystal and enzyme catalyst, crystal is separated with enzyme catalyst.
The manufacture method that preferred embodiment relates to the direct transesterify grease of following above-mentioned record, that is, utilize centrifugation to carry out the sedimentation of enzyme catalyst.
In addition, preferred embodiment relate to the manufacture method of the direct transesterify grease of following above-mentioned record, that is, and more than 1.2 times of the proportion that the proportion of enzyme catalyst is crystal.
In addition, preferred embodiment relate to the manufacture method of the direct transesterify grease of following above-mentioned record, that is, the enzyme catalysis dosage of the particle diameter that 50 μ m are following is with respect to raw oil material 100 weight part less than 1 weight parts.
In addition, preferred embodiment relate to the manufacture method of the direct transesterify grease of following above-mentioned record, that is, making the viscosity of the front reaction grease of enzyme catalyst sedimentation is below 500000cP.
The invention effect
According to the present invention, can effectively obtain the direct transesterify grease of the content that has reduced significantly enzyme catalyst.
In addition, in the present invention, by the enzyme catalyst that will separate with described direct transesterify grease, again with raw oil material, mix, can carry out continuous manufacture.
Embodiment
Below, the present invention will be described in more detail.
The manufacture method of direct transesterify grease of the present invention (following also referred to as manufacture method of the present invention) is characterised in that, in the direct transesterification reaction of using enzyme catalyst, in the raw oil material of enzyme catalyst in reaction system existing by mobile state, do not melt the crystal generated by described reaction, utilize proportion official post enzyme catalyst sedimentation in reacting grease of crystal and enzyme catalyst, crystal is separated with enzyme catalyst.
(raw oil material)
The raw oil material used in the present invention so long as food oils get final product.
It is grease that raw oil material for example can be enumerated palm.As described palm, it is grease, so long as come from just being not particularly limited of palm, palm olein, the palm-kernel oil decile that can exemplify tripalmitin liquefaction, unpurified thick oil, utilizes once raise in above minute carried oil and their winterized stearin, transesterify wet goods.In addition, be grease raw oil material in addition as described palm, can enumerate fractionated oil, winterized stearin, the transesterify wet goods of soybean oil, rapeseed oil, sunflower oil, sweet oil, sesame oil, mustard caul-fat, Oleum Gossypii semen, rice bran oil, Thistle oil, Oleum Cocois, shea butter, sal tree fat, mist ice grass grease, theobroma oil, tallow, lard, butterfat, these greases.
Saturated fatty acid content during the formation lipid acid of described raw oil material is all is preferably below 70 % by weight, more preferably 3～70 % by weight, more preferably 3～52 % by weight.If saturated fatty acid content is greater than 70 % by weight, in the reaction grease that utilizes direct transesterification reaction to obtain, solid fat is too much, and viscosity raises, and therefore has the situation of the separation difficulty of enzyme catalyst and grease.
(enzyme catalyst)
Enzyme catalyst used in the present invention so long as have the lipase of transesterify ability for described raw oil material, just is not particularly limited, and no matter is the random transesterify enzyme that there is no location specific fully, and still having 1,3 specific transesterify enzyme can.But, preferably according to the required palmitinic acid amount of 2, carry out random transesterification reaction or carry out the special transesterification reaction in position and apply in a flexible way.
As described enzyme catalyst, also can use enzyme is fixed on to the pulverous catalyzer on required carrier.As described carrier, so long as do not dissolve in described raw oil material, can get final product with the Powdered material existed, can enumerate cyclodextrin, diatomite, aluminum oxide, celite, Mierocrystalline cellulose and other derivatived cellulose, porous glass, glass fibre, silicic acid gel, florisil silica, ion exchange resin, titanium dioxide, kaolinite, perlite, silicon-dioxide etc., yet, so long as have the function of catching the lipase molecule, its composition just is not particularly limited.
Described enzyme catalyst is so long as Powdered getting final product, but as its particle diameter, if the scope of 100～2000 μ m, treatability is good, in addition, can also effectively carry out the direct transesterification reaction as target.And, as described particle diameter, as long as measure median diameter as putting down in writing in embodiment described later.
As described enzyme catalyst, be greater than the catalyzer of the crystal that utilizes direct transesterification reaction to obtain by using proportion, just can carry out and the separating of the direct transesterify grease that contains crystal etc.
Specifically, for the proportion of described enzyme catalyst, the viewpoint of being separated rapidly from making described enzyme catalyst sedimentation is considered, be preferably more than 1.2 times of proportion of described crystal, more preferably, more than 1.3 times, more preferably, more than 1.5 times, be particularly preferably more than 2 times.
And, in the present invention, use electronic hydrometer (Alfamirage(strain) system) measure the proportion of enzyme catalyst and crystal.
The usage quantity of described enzyme catalyst so long as the amount that direct transesterification reaction is carried out just be not particularly limited, yet from reaction efficiency and economy, consider, with respect to raw oil material 100 weight parts, be preferably 0.5 weight part～20 weight parts.
Wherein, in manufacture method of the present invention, enzyme catalysis dosage by making the particle diameter below 50 μ m is with respect to raw oil material 100 weight part less than 1 weight parts, even by crystal melting, as long as 20 minutes will be remaining with interior utilization filtration etc. the enzyme separation, just random transesterification reaction can be do not made it to occur, the grease of the composition of target can be obtained.
In manufacture method of the present invention, in the raw oil material of described enzyme catalyst in reaction system existing by mobile state.In addition, described enzyme catalyst in carrying out the grease of direct transesterification reaction and in the reaction grease obtained after finishing also all existing by mobile state.Specifically, after adding enzyme catalyst in the material that can in the raw oil material to aqueous, add enzyme catalyst or melt to the raw oil material by solid state heating, utilize be uniformly mixed or with pump etc., reaction tubes etc. is applied to external pressure and make grease by or utilize the method that makes it naturally to fall from eminence etc. to make it mobile.In addition, with regard to stirring, for the grease that uses the devices such as tank with agitating vane or pin-machine to make to be reacted flows, utilizes pump etc. to apply external pressure to reaction tubes etc. and grease is passed through, as long as utilize the mechanism such as static mixer to form, make enzyme catalyst be dispersed in the state in raw oil material.
And, so-called state that can be mobile in the present invention, refer to the meaning of the state be different from as being immobilized of one of previous methods, so long as following state gets final product, that is, enzyme catalyst is dispersed in the raw oil material in reaction system, is also stirred in the situation that stir the raw oil material enzyme catalyst, when standing raw oil material, enzyme catalyst will sedimentation.
(directly transesterification reaction)
No matter the method for the direct transesterification reaction in manufacture method of the present invention is that batch-type or continous way can.
In addition, the direct transesterification reaction temperature while using described enzyme catalyst is so long as just be not particularly limited the temperature of high-melting-point glyceryl ester crystallization, yet in order effectively to be reacted when reaction starts, the temperature that the preferred catalyst activity is the highest.Specifically, be preferably 50 ℃～70 ℃.In addition, from the viewpoint of effectively being reacted, consider, from reaction starts, 3～18 hours, preferably direct transesterification reaction temperature is made as to 0 ℃～40 ℃, more preferably be made as 10 ℃～40 ℃.And, in the present invention, final temperature of reaction is made as to direct transesterification reaction temperature.For example, make it reaction in the situation that be adjusted into the temperature in 2 stages, the temperature of subordinate phase is made as to temperature of reaction.
In addition, by before described direct transesterification reaction, carry out processed, the moisture content in the mixture (being in fact raw oil material) of reduction raw oil material and enzyme catalyst, can be reacted effectively.
As the moisture content in described raw oil material, be preferably below 0.1 % by weight.
In the direct transesterification reaction of manufacture method of the present invention, in the situation that stirred, from raw oil material being given to mobility, being considered from the viewpoint that generates the good crystal of separation property in addition, preferably with 1000rpm(r/min) following speed stirred, 600rpm(r/min more preferably) below, 300～1rpm(r/min more preferably).
For the i.e. crystal amount of crystal before separating with enzyme catalyst just, as long as utilize temperature of reaction and reaction times to control, for example preferably carry out 3～120 hours 0～40 ℃, be preferably the direct transesterification reaction under 10 ℃～40 ℃.Described crystal amount is preferably 3～60 % by weight in reaction grease integral body, more preferably 5～40 % by weight.
For this crystal amount, can be by measuring the SFC(solid fat content of the reaction grease before separating with enzyme catalyst of crystal just) confirm.
And, in the present invention, so-called reaction grease, refer to the grease that carries out direct transesterification reaction and obtain, and refers to the material that solid fat, aqueous grease, raw oil material etc. mix.
In addition, in manufacture method of the present invention, viscosity by making the reaction grease before the enzyme catalyst sedimentation is 500000cP(mPas) below, thus can be according to the content that makes generated crystal or liquid fat many and mode that can operability carry out well the precipitation of enzyme catalyst described later regulated.Described viscosity is preferably 15000cP(mPas) below, 10000cP(mPas more preferably) below, 8000cP(mPas more preferably) below, be particularly preferably 5000cP(mPas) below, the utmost point is preferably 4000cP(mPas) below, most preferably be 3000cP(mPas) below.
The viscosity of described reaction grease can be measured as putting down in writing in embodiment described later.
And, continue direct transesterification reaction unreacted raw oil material reduce, crystal (SSS) content in the reaction grease increases, and in reaction system, because solid fat excessively increases, viscosity is raise, thereby being difficult to carry out carried with dividing of enzyme catalyst.So, from dividing the viewpoint of putting forward efficiency, consider, the SSS content that preferably makes to react in grease is no more than 50 % by weight ground stopped reaction, more preferably make SSS content be no more than 31 % by weight ground stopped reaction, further preferably make SSS content between 1～31 % by weight and stopped reaction, further be preferably 1～25 % by weight, be particularly preferably 1～20 % by weight, most preferably be 1～15 % by weight.
Described direct transesterification reaction is reacted under the described conditions, after confirming the crystal amount, if reach desirable crystal amount, by the separation of carrying out enzyme catalyst, is stopped.
(sedimentation of enzyme catalyst)
In manufacture method of the present invention, after described direct transesterification reaction, do not make generated crystal melting, make enzyme catalyst sedimentation in the reaction grease.Specifically, stop the stirring of described reaction grease and enzyme catalyst, standing under the temperature condition that can not melt at crystal, utilize the difference in specific gravity of crystal and enzyme catalyst, make enzyme catalyst sedimentation in the reaction grease.As described temperature condition, according to the fusing point difference of the crystal of target, can't limit entirely, yet so long as can not cause contrary transesterification reaction as 10～40 ℃, be that the temperature range that generated crystal can not melt gets final product.Utilize this settled process, can realize the Labor-saving of sedimentation operation, yet need about 3～24 hours in the sedimentation of enzyme catalyst.And, if make the viscosity of the reaction grease before the enzyme catalyst sedimentation, be below 4000cP, even consider also sedimentation aptly of productivity.
So, as other method, can carry out rapidly the sedimentation of enzyme catalyst by carrying out centrifugation.As long as temperature during centrifugation is adjusted into the temperature range that can not cause that as 10～40 ℃ contrary transesterification reaction, the crystal generated can not melt.In addition, as long as centrifugal force is above for 1G, if centrifugal force is too high, the crystal stock body also can precipitate, and therefore the yield variation of crystal is preferably 1～10000G.
In the present invention, by after making as described above the enzyme catalyst sedimentation, to reclaim as the direct transesterify grease of supernatant liquor, crystal can be separated with enzyme catalyst thus, make it not contain enzyme catalyst, nor produce the random transesterification reaction of enzyme catalyst or basically prevent the random transesterification reaction of enzyme catalyst.
In addition, by will from described direct transesterify grease, isolated enzyme catalyst former state unchangeably for the direct transesterification reaction of the next one, just carrying out continuous manufacture.
(aftertreatment)
In the direct transesterify grease that utilizes manufacture method of the present invention to obtain, the aqueous grease of the solid fat that contains trisaturated glyceride (SSS) and so on, triunsaturated glyceride (UUU) and so on, therefore preferably by these oil fractionations.
As described minute extracting method, be no matter solvent divide carry or dry fractionation can, yet solvent divides, carry because using solvent to spend cost of equipment, running cost, therefore preferably do not use the dry fractionation of solvent.
In the situation that use solvent, can use hexane, acetone etc.Minute temperature raising degree for dry fractionation, in order with sufficient aqueous property, to obtain aqueous grease, be preferably 0 ℃～30 ℃, more preferably below 20 ℃, if also comprise the viewpoint of yield, and more preferably 0 ℃～10 ℃.
In addition, for improve in solid fat at 2 content with glyceryl ester of palmitinic acid, once preferably after carrying out described dry fractionation, a minute temperature raising degree raises, again divide and carry under 40 ℃～60 ℃, if consider at 2 content and yields with glyceryl ester of palmitinic acid, more preferably under 45 ℃～55 ℃, again divide and carry.
The solid fat obtained in the present invention can or be directly used in the base material etc. of microcapsule for the raw material of the treated oil grease articles such as cream, oleomargarine, shortening, chocolate.In addition, solid fat of the present invention also can be for OPO(2-palmitoyl-1,3-bis-oil base Witepsol W-S 55s) raw material or the PPO(1 of structure grease, 2-bis-palmitoyl-3-bis-oil base Witepsol W-S 55s) in the raw material etc. of structure grease.
In addition, the aqueous grease obtained in the present invention can utilize with the method for being utilized in common aqueous grease as soybean oil, rapeseed oil, the raw material that mainly can be used as seasonings, mayonnaise, cream, oleomargarine, shortening wet goods treated oil grease article utilizes, or can directly as salad oil, frying wet goods, utilize.
The raw material that the solid fat obtained in the present invention and the mixture of aqueous grease can be used as the treated oil grease articles such as cream, oleomargarine, shortening, chocolate utilizes.
Embodiment
Embodiment below is shown, the present invention is carried out to more specific description, yet the present invention is not subject to any restriction of these embodiment.And in embodiment, " part " or " % " take weight as benchmark.
The mensuration of the enzyme catalyst content in the reaction grease of<separation>
Measure the weight of the reaction grease that centrifugation goes out, be heated to 80 ℃ and described grease is fully melted.The hexane that adds 2 times of amounts with respect to described grease, after mixing, utilize Büchner funnel to be filtered.The enzyme catalyst leached is cleaned for several times with hexane, under 40 ℃, after drying, determine the weight of enzyme catalyst.
The median diameter of<enzyme catalyst>
Use laser diffraction/diffuse transmission type particle size distribution device " LA-920HORIBA " to determine the median diameter of enzyme catalyst.
Enzyme catalysis dosage below<particle diameter 50 μ m>
For enzyme catalyst 100g use 400 orders (mesh diameter: sieve 50 μ m), measure the weight of the enzyme catalyst passed through, as the enzyme catalysis dosage below particle diameter 50 μ m.
<viscosity>
The viscosity of reaction grease is that the method for utilizing Corporation Japan oiling to learn record in the 2.2.10.5-1996 viscosity (Brookfield method) of association's volume " benchmark grease analytical method " (publication year: 1996) is measured.
(embodiment 1) settled process
By palm olein (iodine number: 64, proportion 0.91, also all identical in following embodiment) 5000g adds separable flask (four necks, capacity 5L, also all identical in following embodiment) in, carry out vacuum hydro-extraction under 90 ℃ when stirring with 100rpm after, cool to 50 ℃ and add lipase (enzyme catalyst, Novozymes company system " Lipozyme TL IM ": proportion 2.1, also all identical in following embodiment) 500g, described lipase is lowered the temperature after 4 hours 50 ℃ of maintenances with state that can be mobile in palm olein, being stirred, keep in the mobility of described lipase 36 ℃ carry out the direct transesterification reaction of 38 hours after, stop stirring, standing 3 hours, make lipase sedimentation in the reaction grease., reclaim the reaction grease of supernatant liquor, determine enzyme catalysis dosage thereafter.
(embodiment 2) centrifugal separations (89G)
Palm olein 5000g is added in separable flask, when being stirred with 100rpm 90 ℃ carry out vacuum hydro-extraction after, cool to 50 ℃ and add lipase 500g, described lipase is lowered the temperature after 4 hours 50 ℃ of maintenances with state that can be mobile in palm olein, being stirred, keep in the mobility of described lipase 36 ℃ carry out the direct transesterification reaction of 38 hours after, whizzer (the KUBOTA5922 that is 36 ℃ in temperature adjustment by the reaction grease 100g of gained, rotor ST-410M, also all identical in following embodiment) in carry out the centrifugation of 10 minutes with 89G, make the lipase sedimentation., reclaim the reaction grease of supernatant liquor, determine enzyme catalysis dosage thereafter.
(embodiment 3)
Except under 36 ℃, carry out 15 hours, carry out the direct transesterification reaction of 20 hours under 32 ℃, the whizzer temperature adjustment is 32 ℃ beyond, reclaim in the same manner the grease that reacts of supernatant liquor with embodiment 2, determine enzyme catalysis dosage.
(embodiment 4) centrifugal separations (800G)
Palm olein 5000g is added in separable flask, when being stirred with 100rpm 90 ℃ carry out vacuum hydro-extraction after, cool to 50 ℃ and add lipase 500g, described lipase is lowered the temperature after 4 hours 50 ℃ of maintenances with state that can be mobile in palm olein, when being kept the mobility of described lipase stirring, carry out the direct transesterification reaction of 29 hours under 32 ℃ after, carry out the centrifugation of 10 minutes with 800G in the whizzer that is 32 ℃ in temperature adjustment by the reaction grease 100g of gained, make the lipase sedimentation., reclaim the reaction grease of supernatant liquor, determine enzyme catalysis dosage thereafter.
(embodiment 5) centrifugal separations (2000G)
Palm olein 5000g is added in separable flask, when being stirred with 100rpm 90 ℃ carry out vacuum hydro-extraction after, cool to 50 ℃ and add lipase 500g, described lipase is lowered the temperature after 4 hours 50 ℃ of maintenances with state that can be mobile in palm olein, when being kept the mobility of described lipase stirring, carry out the direct transesterification reaction of 29 hours under 32 ℃ after, carry out the centrifugation of 10 minutes with 2000G in the whizzer that is 32 ℃ in temperature adjustment by the reaction grease 100g of gained, make the lipase sedimentation., reclaim the reaction grease of supernatant liquor, determine enzyme catalysis dosage thereafter.
(embodiment 6)
Except carrying out the direct transesterification reaction of 24 hours under 30 ℃, the whizzer temperature adjustment be 30 ℃, reclaim in the same manner the grease that reacts of supernatant liquor with embodiment 4, determine enzyme catalysis dosage.
(embodiment 7)
Except carrying out the direct transesterification reaction of 24 hours under 29 ℃, the whizzer temperature adjustment be 29 ℃, reclaim in the same manner the grease that reacts of supernatant liquor with embodiment 4, determine enzyme catalysis dosage.
The measurement result summary sheet of the enzyme catalysis dosage of the reaction grease that obtains in embodiment 1～7 is shown in Table 1.As shown in Table 1, the enzyme catalyst quantity not sufficient 1% in the reaction grease obtained in embodiment 1～7, significantly reduce.
In addition, calculate the yield ((the reaction oil quantity of the supernatant liquor be recovered to/reaction grease total amount) * 100) of the reaction grease of gained, consequently more than 78%, knownly can from raw oil material, with high yield, obtain the grease of target.
In addition we know, in embodiment 1, because the viscosity that makes the reaction grease before the enzyme catalyst sedimentation is low to moderate 2000cP, although therefore spended time, yet only by the standing enzyme catalysis dosage that just can reduce with respect to the grease after separation.Known on the other hand, even be full-bodied reaction grease as embodiment 6,7, also can be by with centrifugation, effectively separating enzyme catalyst.
[table 1]
* filter stoppage and can not separating
(embodiment 8)
By in embodiment 1 after direct ester reaction from the reaction grease isolated enzyme catalyst be mixed in the raw oil material of new preparation and carry out direct ester reaction under the condition identical with embodiment 1, consequently, obtain the grease that reacts of the composition roughly the same with embodiment 1.So confirm, can be by enzyme catalyst for continuous manufacture.
(comparative example 1)
By palm olein (iodine number: 64, proportion 0.91) 5000g adds separable flask (four necks, capacity 5L, also identical in following comparative example) in, carry out vacuum hydro-extraction under 90 ℃ when stirring with 100rpm after, cool to 50 ℃ and add lipase (enzyme catalyst, Novozymes company system " Lipozyme TL IM ", proportion: 2.1) 500g, described lipase is kept to cooling after 4 hours with state that can be mobile in palm olein under 50 ℃, kept in the mobility of described lipase carrying out the direct transesterification reaction of 38 hours under 36 ℃ stirring after, the decompress filter machine that is 36 ℃ in temperature adjustment (Millipore company system: the net that 860 μ m diameters are set the 90mm disk filter), 100g is carried out to the decompress filter of 60 minutes, separate enzyme catalyst., reclaim the reaction grease of filtrate, determine the enzyme catalysis dosage with respect to the grease after separating thereafter.The results are shown in table 1.
As shown in table 1, in comparative example 1, with the result of embodiment 1, compare, with respect to the enzyme catalysis dosage of the grease after separating, up to about 5.5 times, on the other hand, the yield of reaction grease is less to approximately 0.47 times, therefore it is obviously poor that the method for comparative example 1 is compared the reaction efficiency of enzyme catalyst with the method for embodiment 1, particularly poor because of the separation property of enzyme catalyst, therefore it is also high to produce the possibility of by product, can be described as the method that loss is large.
(comparative example 2)
Except the mesh size of the strainer by the decompress filter machine is made as 250 μ m, reclaim and react grease in the same manner with comparative example 1, determine the enzyme catalysis dosage with respect to the grease after separating.The results are shown in table 1.
As shown in table 1, in comparative example 2, with the result of embodiment 1, compare, enzyme catalysis dosage with respect to the grease after separating is about 1.7 times of left and right, and the yield of reaction grease is little, be about 0.24 times, it is obviously poor that the method that therefore can say comparative example 1 and the method for embodiment 1 are compared reaction efficiency.
(comparative example 3)
Except the mesh size of the strainer by the decompress filter machine is made as 45 μ m, want to reclaim and react grease in the same manner with comparative example 1, yet obstruction has occurred, can't reclaim the reaction grease of having removed enzyme catalyst.
Claims (5)
1. the manufacture method of a direct transesterify grease, is characterized in that,
In the direct transesterification reaction of using enzyme catalyst, enzyme catalyst is can exist by mobile state in the raw oil material in reaction system, do not melt the crystal generated by described reaction, utilize proportion official post enzyme catalyst sedimentation in reacting grease of crystal and enzyme catalyst, crystal is separated with enzyme catalyst.
2. the manufacture method of direct transesterify grease according to claim 1, wherein,
Utilize centrifugation to carry out the sedimentation of enzyme catalyst.
3. the manufacture method of direct transesterify grease according to claim 1 and 2, wherein,
The proportion of enzyme catalyst is more than 1.2 times of proportion of crystal.
4. according to the manufacture method of the described direct transesterify grease of any one in claim 1～3, wherein,
The enzyme catalysis dosage of the particle diameter that 50 μ m are following is with respect to raw oil material 100 weight part less than 1 weight parts.
5. according to the manufacture method of the described direct transesterify grease of any one in claim 1～4, wherein,
Making the viscosity of the front reaction grease of enzyme catalyst sedimentation is below 500000cP.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2011-095543 | 2011-04-21 | ||
| JP2011095543 | 2011-04-21 | ||
| PCT/JP2012/060718 WO2012144599A1 (en) | 2011-04-21 | 2012-04-20 | Method for producing directly transesterified oil or fat |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103492581A true CN103492581A (en) | 2014-01-01 |
Family
ID=47041703
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201280019208.7A Pending CN103492581A (en) | 2011-04-21 | 2012-04-20 | Method for producing directly transesterified oil or fat |
Country Status (3)
| Country | Link |
|---|---|
| JP (1) | JPWO2012144599A1 (en) |
| CN (1) | CN103492581A (en) |
| WO (1) | WO2012144599A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108289469A (en) * | 2015-12-02 | 2018-07-17 | 日清奥利友集团株式会社 | Cladding fat or oil composition |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPWO2013062110A1 (en) * | 2011-10-26 | 2015-04-02 | 株式会社カネカ | Foamable oil-in-water emulsified oil composition for whipped cream |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1079115C (en) * | 1993-09-17 | 2002-02-13 | 日清制油株式会社 | Transesterification method with powdery lipase |
| CN101461423A (en) * | 2009-01-15 | 2009-06-24 | 江南大学 | Method for preparing basic oil of shortening or butterine without granule crystal by ester exchange method |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6078586A (en) * | 1983-10-05 | 1985-05-04 | Lion Corp | Preparation of liquid fat and oil |
| JP2006246808A (en) * | 2005-03-11 | 2006-09-21 | Adeka Corp | Method for carrying out transesterification of oil and fat |
| JP2010068750A (en) * | 2008-09-18 | 2010-04-02 | Fuji Oil Co Ltd | Lipase powder preparation and method for producing the same |
-
2012
- 2012-04-20 JP JP2013511057A patent/JPWO2012144599A1/en active Pending
- 2012-04-20 CN CN201280019208.7A patent/CN103492581A/en active Pending
- 2012-04-20 WO PCT/JP2012/060718 patent/WO2012144599A1/en active Application Filing
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1079115C (en) * | 1993-09-17 | 2002-02-13 | 日清制油株式会社 | Transesterification method with powdery lipase |
| CN101461423A (en) * | 2009-01-15 | 2009-06-24 | 江南大学 | Method for preparing basic oil of shortening or butterine without granule crystal by ester exchange method |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108289469A (en) * | 2015-12-02 | 2018-07-17 | 日清奥利友集团株式会社 | Cladding fat or oil composition |
Also Published As
| Publication number | Publication date |
|---|---|
| JPWO2012144599A1 (en) | 2014-07-28 |
| WO2012144599A1 (en) | 2012-10-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Rossell | Fractionation of lauric oils | |
| CN102858931B (en) | Liquid oil and fat, and production method therefor | |
| CN101939405B (en) | Process for producing a palm oil product | |
| JP5929763B2 (en) | Oil and fat dry separation method | |
| CN102334563A (en) | Method for controlling content of 3-chloro-1,2-propanediol or ester thereof in oil | |
| CN108265089B (en) | Oil and fat composition containing 1, 3-dioleoyl-2-palmitic acid triglyceride and preparation method thereof | |
| CN110016387A (en) | Edible vegetable oil degumming agent and preparation method thereof and refined oil method | |
| JP5161465B2 (en) | Method for producing highly liquid palm oil and highly liquid palm oil | |
| RU2556718C2 (en) | Vegetable oil processing | |
| CN103492581A (en) | Method for producing directly transesterified oil or fat | |
| CN102843914A (en) | Method for purification of edible oil or fat | |
| CN104640963B (en) | The manufacture method of oils and fats | |
| JP2016077175A (en) | Manufacturing method of hard butter | |
| Achaw et al. | Manufacture of crude palm oil and refined palm oil | |
| JP2011193854A (en) | Method for producing water-in-oil emulsified oil and fat composition | |
| US2442535A (en) | Modification of glycerides | |
| CN108239580B (en) | Preparation method of oil containing highly unsaturated fatty acid, obtained oil, and food using the oil | |
| CN102272280B (en) | Method for producing vegetable oil | |
| WO2018097118A1 (en) | Dry-mode oil/fat separation method | |
| JP4887553B2 (en) | Separation of edible oils and fats | |
| CN114761524A (en) | Method for producing purified oil or fat | |
| JP2000204389A (en) | Fractionation of lard | |
| AU2021234620B2 (en) | Dry fractionation of edible oil | |
| JP5308309B2 (en) | Method for producing highly liquid palm oil for cooking | |
| US9296977B2 (en) | Method for producing fatty acid composition |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20140101 |